Patent Grant
7134297
The invention relates to a process for the low-temperature fractionation of air in a rectification unit, which comprises a pressure column, a low-pressure column and a condenser-evaporator system with at least two falling-film evaporators, oxygen-rich liquid from the low-pressure column being introduced into the evaporation passages of the first falling-film evaporator and partially evaporated, and unevaporated oxygen-rich liquid from the first falling-film evaporator being passed into the second falling-film evaporator.
In a low-pressure air fractionation plant having a pressure column and a low-pressure column, liquid oxygen from the low-pressure column is evaporated against gaseous nitrogen from the top of the pressure column by indirect heat exchange, during which the nitrogen condenses. A condenser-evaporator system of this type is generally referred to as the main condenser.
In practice, the main condenser is almost always formed as a circulation condenser or as a falling-film evaporator. In the case of a circulation condenser, the condenser block stands in a bath of the liquid which is to be evaporated. The liquid which is to be evaporated enters the evaporation passages from below and is at least partially evaporated by heat exchange against the heating medium flowing through the liquefaction passages. The gas which is formed during the evaporation entrains liquid from the bath into the evaporation passages. This thermosiphon effect results in the formation of a natural circulation of liquid through the circulation condenser without there being any need for further means for conveying liquid.
By contrast, in the case of a falling-film evaporator, the liquid which is to be evaporated is introduced into the evaporation passages from above via a distribution system, which simultaneously forms a gas closure. The liquid runs downwards along the walls which separate the evaporation passages and the liquefaction passages as a film of liquid and is partially evaporated. The vapour which is formed and the unevaporated residual liquid emerge from the falling-film evaporator at the bottom. This type of evaporator has a particularly low pressure loss in the evaporation passages and therefore in terms of energy is generally more suitable than a circulation evaporator.
However, when an oxygen-rich liquid is being evaporated, total evaporation, which causes the evaporation passages to run dry, must be prevented. For this purpose, it is generally the case that a significantly larger quantity of liquid than is actually to be evaporated is added to the evaporation passages, so that in addition to the desired vapour there is always a certain quantity of excess liquid which emerges from the evaporation passages. However, delivering excess liquid to the evaporation passages runs contrary to the energy-saving effect of the falling-film evaporator.
In EP-A 0 926 457, it is proposed for two or more falling-film evaporators to be arranged above one another between the bottom of the low-pressure column and the lowermost mass transfer elements of the low-pressure column. The individual falling-film evaporators are arranged in series. The oxygen-rich liquid which emerges from the mass transfer elements is collected and introduced into the first falling-film evaporator. Unevaporated liquid from the first falling-film evaporator is then transferred into the second falling-film evaporator arranged below it. There is no provision for liquid to be recirculated from the bottom of the low-pressure column into the falling-film evaporators.
In the event of load changes, the ratio of the liquid dropping out of the low-pressure column and the gaseous nitrogen formed at the top of the pressure column may change, at least temporarily. In the condenser-evaporator system described in EP-A 0 926 457, this can lead to the ratio of the liquid which enters the evaporation passages to the heating medium flowing in the evaporation passages decreasing. In the event of such a lack of equilibrium between the quantities of heating medium and lipid to be evaporated, the evaporation passages may run dry and relatively low-volatility substances can accumulate therein.
U.S. Re. 36,435 has likewise disclosed a low-temperature fractionation plant with two falling-film evaporators arranged above one another. To start up the plant, only the upper falling-film evaporator is fed with liquid from the bottom of the low-pressure column, while only the liquid which emerges from the first evaporator enters the downstream falling-film evaporator. In normal operation, by contrast, liquid from the bottom of the low-pressure column is only pumped into the lower falling-film evaporator. The upper evaporator is fed only with the liquid which emerges from the mass transfer elements of the low-pressure column. In a plant of this type, the problem exists that undefined quantities of fluid are fed to the upper falling-film evaporator, in particular in the event of load changes, with the result that the evaporation passages, as described above, may run dry.
In the case of relatively large air fractionation plants, which are equipped with more than one falling-film evaporator, therefore, hitherto the individual falling-film evaporators have been connected and operated not in series but rather in parallel. For this purpose, however as described above, a corresponding quantity of excess liquid has to be pumped to each falling-film evaporator, which has an adverse effect on the energy balance.
Therefore, the present invention is based on the object of providing a process of the type described in the introduction which is particularly favourable in terms of energy and operating technology and in which the accumulation of relatively low-volatility substances in the falling-film evaporators is avoided.
This object is achieved by a process of the type described in the introduction, in which oxygen-rich liquid from the bottom of the low-pressure column is introduced into the evaporation passages of the first falling-film evaporator and into the evaporation passages of the second falling-film evaporator.
According to the invention, the evaporation passages of the second falling-film evaporator are fed with unevaporated liquid from the first falling-film evaporator. For safety reasons, in order to prevent the falling-film evaporator from running dry, liquid from the bottom of the low-pressure column is fed into the evaporation passages of the first falling-film evaporator. Total evaporation of the liquid also has to be avoided in the evaporation passages of the second falling in evaporator. In this context, it is possible to supply the first falling-film evaporator with so much liquid from the bottom of the low-pressure column that sufficient unevaporated liquid remains to be passed on to the second falling-film evaporator.
According to the invention, however, so much liquid is added to the first falling-film evaporator that it does not run dry, even when a safety factor is taken into account. The second falling-film evaporator is supplied firstly with unevaporated liquid from the first falling-film evaporator and secondly with a suitable quantity of liquid from the bottom of the low-pressure column, so that it is prevented from running dry.
The mixture of generated vapour and unevaporated liquid which emerges from the first falling-film evaporator is advantageously separated into a fraction which substantially includes vapour and a traction which substantially includes liquid. Only the liquid is passed on into the second falling-film evaporator. The vapour fraction is returned to the low-pressure column or removed from the plant as gaseous product.
Of course, the invention is not restricted to just two falling-film evaporators being arranged in series one behind the other. Depending on the type and size of plant, it has also proven favourable for three or more falling-film evaporators to be arranged in series, i.e. for the unevaporated liquid which emerges from the second falling-film evaporator to be fed to a third falling-film evaporator. Furthermore, it may be advantageous if one or more further falling-film evaporators are connected in parallel with respect to the first and/or second falling-film evaporators. In this case, the liquid which emerges from the first falling-film evaporator and all the falling-film evaporators which are connected in parallel therewith is preferably combined and distributed to the second falling-film evaporator and any falling-film evaporators arranged in parallel therewith.
It is advantageous for the amount of oxygen-rich liquid fed to the first and second falling-film evaporators to be two to five times the amount of oxygen in vapour form produced in the corresponding falling-film evaporator. This procedure ensures that running dry i.e. total evaporation of the liquid oxygen, cannot occur. For the second falling-film evaporator, it is merely necessary to add the amount of liquid which has evaporated in the first falling-film evaporator from the bottom of the low-pressure column. In other words, two to five times as much liquid from the bottom of the low-pressure column is fed to the first falling-film evaporator as to the second falling-film evaporator.
It is preferable for the individual falling-film evaporators to be arranged in such a way that the liquid which emerges from the first falling-film evaporator flows into the second falling-film evaporator without the use of a pump, purely under the force of gravity. Of course, a corresponding statement is also true for the flow communication between the second falling-film evaporator and any third falling-film evaporator.
Furthermore, the falling-film evaporators are preferably arranged in such a way that the condensed nitrogen which emerges from the second (or third) falling-film evaporator flows back into the pressure column on account of static pressure and the unevaporated liquid oxygen which emerges from the second (or third) falling-film evaporator flows back into the low-pressure column on account of static pressure, in order to save on pumps or other delivery devices.
The intention and further details of the invention are explained in more detail below with reference to exemplary embodiments illustrated in the drawing, in which:
Gaseous nitrogen is extracted at the top of the pressure column 1 via line 5 and is introduced via the lines 6 and 7 into the respective liquefaction passages of the falling-film evaporators 3 and 4, respectively. The nitrogen which emerges from the liquefaction passages of the two falling-film evaporators 3, 4 is then fed back to the top of the pressure column 1 as reflux liquid via the lines 8 and 9, respectively. The falling-film evaporators 3, 4 are arranged in such a way that after the condensation in the falling-film evaporators 3, 4, the nitrogen can run back into the pressure column 1 with a gradient, without a pump being required.
The oxygen-rich liquid which accumulates in the bottom 10 of the low-pressure column 2 is conveyed upwards to the two falling-film evaporators 3, 4 via line 12 with the aid of a pump 11 and is throttled into a level vessel 20 which is connected to the upper header 31 of the corresponding falling-film evaporator 3, 4. A certain liquid level above the evaporation passages is maintained in the level vessel 20. This level firstly provides the required static pressure in order to convey the vapour which is formed in the evaporation passages and the unevaporated liquid downwards through the evaporation passages. Secondly, this liquid level ensures that no vapour from the top space of the falling-film evaporators 3, 4 enters the corresponding evaporation passages.
The oxygen-rich liquid is partially evaporated in the evaporation passages. The vapour-liquid mixture is then returned to the low-pressure column 2 via line 13. A further line 14, via which oxygen in vapour form can be removed as product of the plant, branches off from line 13. A line 30 which connects the upper and lower headers 31 of the two falling-film evaporators 3, 4 is used to compensate for any excess or reduced pressure in one of the headers 31.
To prevent the two falling-film evaporators 3, 4 from running dry, they are operated with an excess of oxygen-rich liquid. By way of example, 100,000 m3/h (s.t.p.) of oxygen are evaporated in the main condenser, i.e. 50,000 m3/h (s.t.p.) of oxygen are produced in each falling-film evaporator 3, 4. For safety reasons, three times the quantity of liquid oxygen, i.e. in each case 150,000 m3/h (s.t.p.), are applied to the falling-film evaporators 3, 4. In total, therefore, 300,000 m3/h (s.t.p.) of liquid oxygen are delivered by the pump 11 from the bottom 10 of the low-pressure column 2 to the top of the falling-film evaporators 3, 4. In this example, the height of the pressure column should be 14 m and the falling-film evaporators 3, 4 should each be 8 m high. The pump 11 therefore has to deliver 300,000 m3/h (s.t.p.) of liquid oxygen to a total height of 14 m+8 m=22 m.
The liquid oxygen which is extracted from the bottom 10 of the low-pressure column 2 is partly pumped via line 215 to the top of the falling-film evaporator 203 and partly pumped via line 216 to the top of the falling-film evaporator 204. An excess of liquid oxygen which has not been evaporated emerges at the bottom end of the evaporation passages of the upper falling-film evaporator 203. The vapour produced and the excess liquid are separated in the separator 219. The excess liquid is then added to the top of the falling-film evaporator 204 via line 217, while the vapour produced is returned to the low-pressure column via the lines 232 and 218 or partially extracted as product via line 214. Line 230 is used for pressure compensation between the upper and lower ends of the falling-film evaporator 203.
The falling-film evaporator 204 is fed with the excess liquid from the upper falling-film evaporator 203 via line 217 and with fresh liquid via line 216. The vapour-liquid mixture which emerges from the evaporation passages of this evaporator 204 is returned to the low-pressure column 2 via line 218.
The boundary conditions for the air fractionation plant shown in
150,000 m3/h (s.t.p.) of liquid oxygen have to be added to the upper falling-film evaporator 203. 50,000 m3/h (s.t.p.) of oxygen vapour and 100,000 m3/h (s.t.p.) of excess liquid are produced at the bottom end of this falling-film evaporator 203. 50,000 m3/h (s.t.p.) of liquid oxygen is admixed to this 100,000 m3/h (s.t.p.) of excess liquid and is delivered to this point by the pump 211. The mixture of excess liquid from the falling-film evaporator 203 and fresh oxygen is added to the lower falling-film evaporator 204. The lower falling-film evaporator 204 likewise delivers 50,000 m3/h (s.t.p.) of oxygen in vapour form and 100,000 m3/h (s.t.p.) of excess liquid.
In this case, the pump 211 has to deliver a total of 200,000 m3/h (s.t.p.) of liquid oxygen. However, the overall delivery height is greater than with the arrangement shown in
The pump energy is proportional to the product Of the quantity of liquid and the total deliver height. The ratio of the pump energies in the arrangements show in
(300,000 m3/h (s.t.p.)*22 m)/(200,000 m3/h (s.t.p.)*30 m)=1.1.
Therefore, in the arrangement which is known in the prior art and is shown in
Overall, once again 100,000 m3/h (s.t.p.) of oxygen in vapour form, i.e. 33,333 m3/h (s.t.p.) of vapour in each falling-film evaporator 403, 404, 421, are to be produced. The quantity applied to the individual falling-film evaporators 403, 404, 421 should likewise once again amount to a factor of three.
Therefore, 100,000 m3/h (s.t.p.) of liquid oxygen from the bottom 10 of the low-pressure column 2 have to be delivered to the falling-film evaporator 403. The result at the bottom end of the falling-film evaporator 403 is 33.333 m3/h (s.t.p.) of oxygen in vapour form and 66,666 m3/h (s.t.p.) of liquid oxygen. Therefore, a further 33,333 m3/h (s.t.p.) of fresh oxygen have to be added to the falling-film evaporator 404 via line 416. Likewise, 33,333 m3/h (s.t.p.) of oxygen in vapour form and 66,666 m3/h (s.t.p.) of liquid oxygen are produced at the bottom end of the evaporator 404, so that it is also necessary for 33,333 m3/h (s.t.p.) of liquid Oxygen to be fed to the bottom falling-film evaporator 421 by means of the pump 411. In total, therefore, 166,666 m3/h (s.t.p.) of liquid oxygen have to be pumped over a total height of 14 m+8 m+8 m+8 m=38 m. Compared to three falling-film evaporators arranged in parallel (delivery quantity=300,000 m3/h (s.t.p.); total delivery height=14 m+8 m=22 m), the radio of the corresponding pump energies tuns out to be
(300,000 m3/h (s.t.p.)*22 m)/(166,666 m3/h (s.t.p.)*38 m)=1.046.
Therefore, compared to the conventional parallel arrangement of three falling-film evaporators, the result is an energy saving of almost 5%.
The following table shows the pump energy ratios for different pressure column heights of between 14 m and 24 m when the falling-film evaporator arrangement according to the invention is used compared to the conventional arrangement. The relative energy consumption with a parallel arrangement with the falling-film evaporators (one level), the inventive arrangement of two falling-film evaporators in series one above the other (two levels) and an inventive arrangement of three falling-film evaporators in series one above the other (three levels) is compared. The energy demand is in each case standardized with respect to the use of two falling-film evaporators (two levels) connected in series with a pressure column height or 14 m. The overall height of the falling-film evaporators is assumed to be 8 m.
Table 2 once again shows the energy demand of the pump as a function of the pressure column height, the variant having two levels being standardized to 1 for each pressure column height. The values entered in the “1 level” and “3 levels” columns therefore directly show the energy ratio of the respective arrangement to the corresponding arrangement with two falling-film evaporators connected in series.
It is clearly apparent that the arrangement according to the invention of two or more falling-film evaporators above one another provide energy benefits for all pressure column heights. In addition to the energy savings shown, the invention has the further advantage that a smaller and therefore less expensive pump can be used, since smaller quantities of liquid have to be delivered.
| Number | Date | Country | Kind |
|---|---|---|---|
| 102 05 878 | Feb 2002 | DE | national |
| 02009897 | May 2002 | EP | regional |
| Number | Name | Date | Kind |
|---|---|---|---|
| 4606745 | Fujita | Aug 1986 | A |
| 5122174 | Sunder et al. | Jun 1992 | A |
| 5699671 | Lockett et al. | Dec 1997 | A |
| RE36435 | Grenier et al. | Dec 1999 | E |
| 6351968 | Habicht et al. | Mar 2002 | B1 |
| Number | Date | Country |
|---|---|---|
| 0 926 457 | Jun 1999 | EP |
| Number | Date | Country | |
|---|---|---|---|
| 20040055331 A1 | Mar 2004 | US |
